Process for the preparation of 2,6-dialkylphenols

ABSTRACT

This invention discloses a process for the preparation of 2,6dialkylphenols which comprises reacting cyclohexanone with either formaldehyde or acetaldehyde in the vapor phase at a temperature of from 150* to 850* C. in the presence of a particular catalyst. As a catalyst, a compound of metals of Group Ia of the Periodic Table of the Elements is employed in this invention, and a compound of metals of Group IVa and Va of the Periodic Table of the Elements may be employed, as a promotor, together with the above mentioned catalyst for the purpose of increasing the yield and selectivity of the product. In contrast with the conventional methods, the present process can be economically and simply carried out to produce 2,6dialkylphenol in high yield with a great industrial advantage.

United States Patent Izawa et al. 1 June 13, 1972 s41 PROCESS FOR THE PREPARATION OF 3,514,492 5/1970 .luguin et al ..260/62l 1-1 2,6-DIALKYLPHENOLS 3,534,110 10/1970 Juguin m1 ..260/621H [72] Inventors: Shin-[chi Izawa; Katsuyukl Nakamura, both of Tokyo; Yoshiyuki Mizoguchl, Iruma-gun, all of Japan [73] Assignee: Asahikasei Kogyo Kabushiki Kaisha,

Osaka, Japan [22] Filed: April 23, 1969 21 App]. No.: 818,776

[30] Foreign Application Priority Data May 2, 1968 Japan ..43/83622 May ll, 1968 Japan ..43/836l8 [52] US. Cl. ..260/62l R, 260/624 C [51] ..C07c 37/12 [58] Field of Search ..260/621, 621 H, 624 C, 621 R [5 6] References Cited UNITED STATES PATENTS 3,280,201 10/1966 Hamilton et a1 ..260/62l R Primary Examiner-Hemard Helfin Assistant Examiner-Norman Morgenstem Attorney-Oldham & Oldham [57] ABSTRACT This invention discloses a process for the preparation of 2,6- dialkylphenols which comprises reacting cyclohexanone with either formaldehyde or acetaldehyde in the vapor phase at a temperature of from 150 to 850 C. in the presence of a particular catalyst.

As a catalyst, a compound of metals of Group la of the Periodic Table of the Elements is employed in this invention, and a compound of metals of Group IVa and Va of the Periodic Table of the Elements may be employed, as a promotor, together with the above mentioned catalyst for the purpose of increasing the yield and selectivity of the product.

In contrast with the conventional methods, the present process can be economically and simply carried out to produce 2,6-dialkylphen0l in high yield with a great industrial advantage.

6 Claims, No Drawings PROCESS FOR THE PREPARATION OF 2,6- DIALKYLPHENOLS This invention relates to a process for the preparation of 2,6-dialkylphenol and more particularly relates to a process for the preparation of 2,6-dialkylphenol which comprises reacting cyclohexanone with either formaldehyde or acetaldehyde in the vapor phase in the presence of a particular catalyst.

2,6-dialkylphenols have increased in importance as the raw materials for novel synthetic resins, for example, polyphenylene oxide in the plastics field.

There have been many known methods for the preparation of 2,6-dialkylphenol. For example, there is a method by methylation of phenol (Japanese Pat. Publication Nos.6894/ 1967 and 8255/1968), a method by debutylation of 2,6-demethyl-4-t-butylphenol (Netherlands Pat. No.290,847; Japanese Pat. Publication No.7450/ 1967), a method by vapor phase reaction of cyclohexanone with formaldehyde or acetaldehyde (French Patent No.l,377,943; Belgian Pat. No. 641,864; US. Pat. No.3,280,20l etc.

After the detailed invenstigation about the vapor phase reaction of cyclohexanone with either formaldehyde or acetaldehyde, we have unexpectedly found that a compound of metals of Group la of the Periodic Table of the Elements is more effective, as a catalyst, than other known catalysts to produce 2,6-dialkylphenol.

Further we have discovered that the yield and selectivity of 2,6-dialkylphenols are remarkably improved by employing a compound of metals of Group lVa and Va of the Periodic Table of the Elements, as a promotor, together with the above mentioned catalyst.

The compounds of metals of Group Ia of the Periodic Table of the Elements which are used as catalysts in this invention includes carbonates, bicarbonates, nitrates and oxides of a metal selected from the group consisting of lithium, sodium, potassium, rubidium and cesium and a compound of the general formula MOX, wherein M represents metals of the Group la of the Periodic Table of the Elements and X represents hydrogen, a lower alkyl radical, an aryl radical or an acyl radical Examples of the compounds of metals of Group la of the Periodic Table of the Elements include lithium carbonate, sodium carbonate, potassium carbonate, rubidium carbonate, cesium carbonate, lithium bicarbonate, sodium bicarbonate, potassium bicarbonate, rubidium bicarbonate, cesium bicarbonate, lithium nitrate, sodium nitrate, potassium nitrate, rubidium nitrate, cesium nitrate, lithium oxide, sodium oxide, potassium oxide, rubidium oxide, cesium oxide, lithium hydroxide, sodium hydroxide, potassium hydroxide, rubidium hydroxide, cesium hydroxide, lithium methoxide, sodium methoxide, potassium methoxide, lithium phenoxide, sodium phenoxide, potassium phenoxide, sodium formate, lithium acetate, potassium acetate, sodium acetyl acetonate, sodium salt of ethyl acetoacetic acid and the like.

The preferred amount of the catalyst ranges from 0.01 to lOg. base on lg. of the flowing volume of starting raw material per hour and the above mentioned catalysts may be mixtures of two or more compounds.

The compounds of metals of Group [Va and Va of the Periodic Table of the Elements which are used as promotors in the process of this invention includes carbonates, oxides, formates, acetates, oxalates, halides and nitrates of metals of Group [Va and Va of the Periodic Table of the Elements,

especially germanium, tin, lead, arsenic, antimony and bismuth.

Examples of these compounds include tin(ll)oxide,

tin( ll)nitrate and bismuth( Ill )nitrate.

These promotors may also be used as mixtures of two or more of the above mentioned compounds.

The preferred amount of the promoter ranges from 0.5 to 20 weight percent of the catalyst.

In carrying out the reaction of this invention, it is ad-' vantageous to support the catalyst on a carrier in order to improve the toughness of the catalyst and catalyst-life. Typical examples of the carrier include silica-gel, alumina, activated carbon, silica-alumina, zinc oxide, boria and silica-boria.

In practicing the reaction of this invention, the catalyst which may be supported on the above mentioned carrier is ,preferably pre-heated to the reaction temperature and thereafter cyclohexanone and either formaldehyde or acetaldehyde are passed through the pre-heated catalyst.

In order to efl'ect the reaction in vapor phase, the reaction temperature of this invention is in a range of from to 850 C., preferably 250 to 650 C., and the reaction is carried out at atmospheric, subatmospheric or superatomospheric pressure.

To produce 2,6-dimethylphenol, known as 2,6-xylenol, by the reaction of this invention, formaldehyde is reacted with cyclohexanone. If 2,6-diethylphenol is the desired productf acetaldehyde is reacted with cyclohexanone.

In the reaction of cyclohexanone with the aldehyde to produce 2,6-dialkylphenol, 2 moles of the aldehyde are I theoretically required for 1 mole of cyclohexanone. But the molar ratio of the aldehyde and cyclohexanone to effect the reaction of this invention varies in accordance with the kind of aldehyde and the reaction conditions. In general, at least 2 moles of the aldehyde are required for 1 mole of cyclohexanone in this invention. However, using 3 to 10 moles of the aldehyde to 1 mole of cyclohexanone is preferable due to the ease in operating the reaction and the economics of the process.

In carrying out the reaction of this invention, the reactants may be sent into a reaction system together with certain preheated gases (such as nitrogen, carbon monoxide, carbon dioxide, steam, argon, helium) in order to accelerate vaporization.

According to the process of the present invention, 2,6-dialkylphenol is produced with a high yield and selectivity and can be easily separated and purified from by-products such as monoalkylphenol, trialkylphenol or 2,4-dimethylphenol.

It will be understood from the following Table 1 that inorganic compounds of metals other than Group la of the Periodic Table of the Elements are less effective in yield and selectivity of 2,6-dialkylphenol than the catalyst of this invention.

It will be also understood from the following Table 2 that a promotor other than that of the present invention has little or no beneficial effect on the efficiency or selectivity of the 2,6- dialkylphenol preparation.

TABLE 1 Ratio of Conver- Yield based on cyclohexanone recovery sion of (mole percent) of liquid cycloproducts hexanonc 2,6-d1- 2,4di- 2,4,6-trl- Comparative (weight (mole methylmethylmethylexample number Catalyst percent) percent) o-Cresol phenol phenol phenol l C9,;(PO4): 30 U5 7 11 l l 2 Active carbon 4G 84 8 24 2 .1 O ctlvc carbon (20% by weight) i7 10!) 20 17 5U 96 ll 3 4 2 is 77 3 a s 1 TABLE l-Continued Ratio of Conver- Yield based on eyclohaxanono recovery sion (mole percent) of liquid cycloproducts hexnnone 2,6-di- 2,4-dl- 2,4,6-trl- Comparative (weight (mole inothyliuethylmethylcxamplo number Catalyst percent) percent) o-Crosol phenol phenol phenol 35 85 l 5 13 10 48 71 5 2 2...... 7U 4U l l3 2 30 J 8 .2 4 1 30 88 .2 l0 2 65 50 i3 13 J 3 Reaction conditions: Catalyst, 15 ml.; ml./hr.; reaction temperature, 450 0; reaction time, 8 hours.

reactant composition, fcrrnaldehyde/cyclohexanone=3 (by mole ratio); flow rate, 15

TABLE 2 Yield based on cyclohexanone (mole Ratio of Conpercent recovery version of liquid of Cyclo- 2,6- 24- 2,4,6 Promoter products hexanone didi tri Comparative (mole (weight (mole methylmethylmethylexample number Catalyst percent) percent) percent) o-Cresol phenol phenol phenol B2O33H2O2 79 98 18 42 8 1 V 0 82 95 9 63 2 M001 90 99 8 70 4 3 MnSOr 80 100 54 8 2 Th0: 81 99 6 64 2 1 Ci'O 85 98 4 40 17 3 NlSOi 90 100 4 71 3 3 T101 81 99 13 41 13 Reaction Conditions: Catalyst, ml.; reactant composition, formaldehyde/eyclohaxanone=3 (by mole Formalin at a molar ratio of cyclohexanone to formaldehyde of 1 to 4 was introduced into an 800 mm long quartz U-shaped tube of mm inside diameter packed with 15g of the resulting catalyst and maintained at 600 C. in a fluidized bath at a flow rate of 15 ml./hr. for 8 hours while passing therein nitrogen at a flow rate of 180 ml./min. The reaction products were collected in a receiver cooled with water and dryicemethanol.

Another run was operated using, as catalyst, 15g of alumina after heat treatment at 650 C. The results are shown in Table 3.

When alumina alone was used as catalyst the rate of recovery of liquid products was much lower due to the decomratio); fiow rate, 15 ml./hr.; reaction temperature, 450 0.; reaction time, 8 hours.

The features of the present invention can more fully be un- 2,4-Dim cthylphcnol 7.3 L8 derstood by the following non-limiting illustrative examples in gg z gm g 3 g which parts are all by weight and percents are all mole percent y p cm unless expressly slated to the contrary- Ratio of recovery of liquid 58.5 88.9

products (weight EXAMPLE 1 Two hundred grams of alumina was immersed in 100 ml. of EXAMPLE 2 a 5 percent aqueous potassium hydrogen carbonate solution i and the whole mixture was evaporated to dryness and calcined The effect of methanol Formal! m the reactant Sohmon at An aqueous Solution containing cyclohexanone and was invenstigated using, as catalyst, silica-alumina and sodium carbonate supported on silica-alumina. Five hundred grains of silica-alumina was immersed in 200 ml. of a 5 percent aqueous sodium carbonate solution and the whole mixture was evaporated to dryness and calcined at 550 C. for 4 hours. An aqueous solution containing cyclohexanone, formaldehyde and methanol at a molar ratio of l:4:0.l was introduced into the same reaction tube as in Example I packed with 15g of the resulting catalyst and maintained at 350 C. at a flow rate of 15 ml./hr. for 8 hours. This run was repeated in the absence of methanol. Another run was conducted using, as catalyst, 15g of alumina after heat treatment at 650 C. in the absence of methanol. The results are tabulated in Table 4.

TABLE 4 position of the reactants. A large amount of carbon monoxide, carbon dioxide, methane, ethane and ethylene was observed Pf Y in the vapor after the reaction. Furthermore, the formation of 'l ii i Liquid Products alumina Silica- Silicaphenol by dehydrogenation of cyclohexanone, m-cresol and p- 9 alumina: alumina: cresol besides o-cresol, 2,4-dimethylphenol and 2,4,6- dimeth l henol was remarkable and uentl y p conseq y.the sel.ec Cyclohexanol l0.3 0.4 0.5 tivity was very low. In contrast, when a potassium oxide Phenol M6 L4 L4 catalyst supported on alumina was used the selectivity of 2,6- .0 1 23114.2 14.3 dimethylphenol was markedly improved and 2,6-

g ll -g l g 3 me y p e110 dimethylphenol was obtained with a high yield. 24 Dimemylphem| 1 L0 0.6 04

Other dimethylphenols 0.3 TABLE 3 2,4,6'Trimethylphenol 3.0 2.0 2.0 C talyst Others 16.1 0.8 1.! 3 Ratio of recove of li uid 70.3 94.3 94.8 Liquid Products A50, K,0Al,0s d ts (weigh 3%) q 70 Cyclohexanone 5.5 0.4 C l h l 1.7 gg z 359 2 Note: l Absence of methanol o-Crcsol l8.9 13.4 (2) Prcsence meihaml m-Cresol 8: p-Cresol 12.3 0 2,6;Dig ethylphenol 7 5 7 74.3 EXAMPLE;

Five hundred grams of active carbon was immersed in a methanol aqueous solution containing 0.1 mol of sodium phenoxide and the whole mixture was evaporated to dryness and further dried at 400 C. in a nitrogen atmosphere to activate the catalyst. Fifieen grams of this catalyst was filled in the same reaction tube as in Example 1 and the reaction was effected at 250 C. for 8 hours. Eighty four grams of liquid products were collected and the organic layer separated from the liquid products was found to contain 70.3% of 2,6- dirnethylphenol, 11.3% of o-cresol and 1.3% of 2,4,6- trimethylphenol by analysis with a gas chromatograph.

EXAMPLE 4 Two grams of lithium hydroxide was supported on 300g of silica alumina zinc oxide at a weight ratio of l to 3 and the whole was calcined at 400 C. for 2 hours. Fifteen grams of this catalyst was filled in the same reaction tube as in Example 1 and the reaction was efiected at 400 C. for 6 hours in the same manner as in Example 1. Sixty-four grams of liquid products were collected and the organic layer separated from the liquid products was found to contain 65.2% of 2,6- dimethylphenol, 18.5% of o-cresol and 3.3% of 2,4,6- trimethylphenol by analysis with a gas chromatograph.

EXAMPLE 5 Eight hundred grams of silica gel was added to 500 ml. of a 5 percent aqueous solution of cesium carbonate and sodium carbonate at a weight ratio of l to 5 and the whole was evaporated to dryness and calcined at 450 C. for 2 hours to obtain a cesium-sodium catalyst supported on silica gel. Fifteen grams of this catalyst was filled in the same reaction tube as in Example 1 and the reaction was effected at 450 C. for the specified time in the same manner as in Example 1. The

Two hundred grams of silica gel was immersed in 100 ml. of a 5 percent aqueous solution of sodium carbonate and the whole mixture was evaporated to dryness and thereafter calcined at 600 C. for 4 hours. Fifteen grams of this catalyst was filled in the same reaction tube as in Example 1 and a mixed aqueous solution containing three parts of acetaldehyde and 1 part of cyclohexanone was introduced to the reaction tube at 500 C. for 8 hours in the same manner as in Example 1. Ninety one grams of liquid products were collected and the organic layer separated from the liquid products was found to contain 68.5% of 2,6-diethylphenol, 13.8% of o-ethylphenol and 5.3% of triethylphenol by analysis with a gas chromatograph.

EXAMPLE 7 Two hundred grams of silica-lead(ll)oxidi at aweight ratio of 10 to l was immersed in 150 ml. of a 5 percent aqueous solution of potassium carbonate and the whole mixture was evaporated to dryness and thereafter calcined at 450 C. for 2 hours. Fifteen grams of this catalyst was filled in the same reaction tube as in Example 1 and a mixed aqueous solution containing four parts of acetaldehyde and 1 part of cyclohexwas found to contain 72.3% of 2,6-diethylphenol, 14.6% of oethylphenol and 4.3% of triethylphenol on the average.

EXAMPLE 8 To 200g of silica sol there were added an aqueous sodium carbonate solution containing 0.05 mol of sodium carbonate [and then an aqueous arsenic acid solution containing 0.01 mol of arsenic acid. Thereafter to the resulting mixture there was added 20g of alumina sol and the whole gel was evaporated to dryness under reduced pressure, calcined at 500 C. for 5 hours and pulverized. Fifteen milliliters of this catalyst was filled in an 800 mm. long quartz tube of 20 mm. inside diameter, which was preheated at 380 C. for 2 hours. Two hundred milliliters of aqueous solution containing 9.5g of formaldehyde and l0.5g of cyclohexanone was continuously passed ;thereto at a flow rate of 20 ml./hr. for 8 hours. 150.3g of liquid products were collected and the organic layer separated from 'the liquid products was found to contain 86.2% of 2,6- dimethylphenol, 10.3% of o-cresol and 2.0% of 2,4,6- trimethylphenol by analysis with a gas chromatograph.

EXAMPLE 9 The catalyst was prepared in the same manner as in Example 8 using 0.02 mol of fine powder gennanium oxide instead of arsenic acid. The reaction was effected using 15 ml. of this catalyst at 350 C. for 3 hours in the same manner as in Example 8. 58.5g of liquidproducts were collected and the organic layer was found to contain 83.2% of 2,6-dimethylphenol, 12.3% of o-cresol and 1.6% of 2,4,6-trimethylphenol.

Example 10 To 100g of silica sol there were added an aqueous solution containing 0.05 mol of lead(ll)nitrate and an aqueous solution containing 0.025 mol of potassium hydroxide. The whole mixture was evaporated to dryness under reduced pressure and thereafter calcined at 600 C. for 5 hours to activate the catalyst. Fifteen milliliters of this catalyst was charged in a quartz U-shaped tube of 20 mm. inside diameter and 800 mm. length and the same reactant solution as in Example 8 was introduced into the reaction tube at a flow rate of 15 ml./hr. for 10 hours at 550 C. 126.8g of liquid products were collected and the organic layer separated from the liquid products was found to contain 87.3% of 2,6-dimethylphenol, 9.1% of ocresol and 0.8% of 2,4,6-trimethylphenol.

EXAMPLE 1 1 To 600g of silica so] there were added an aqueous solution of 0.1 mol of tartar emetic and diluted hydrochloric acid and the whole mixture was evaporated to dryness at a temperature ranging from 70 to C. under reduced pressure, calcined at 500 C. for 6 hours, pulverized, immersed in a l N potassium carbonated solution at a temperature of 50 to 60 C., filtered off and again calcined at 500 C. for 6 hours. Two hundred milliliters of an aqueous solution containing 23g of formaldehyde and 10g of cyclohexanone was continuously introduced into the same reaction tube as in Example 8 packed with 15 ml. of the resulting catalyst at a flow rate of 10 ml./hr. for 6 hours in the same manner as in Example 8. 58.4g of liquid products were collected and the organic layer separated from the liquid products was found to contain 88.3% of 2,6- dimethylphenol, 8.2% of o-cresol and 1.4% of 2,4,6- trimethylphenol by analysis with a gas chromatograph.

EXAMPLE 12 One hundred grams of silica gel was immersed in an aqueous solution of 0.03 mol of potassium stannate and the whole mixture was lefl to stand overnight, evaporated to dryness, calcined at 550 C,, immersed in ml. of a 3% aqueous solution of potassium carbonate, evaporated to dryness and again calcined at 550 C. An aqueous solution containing cyclohexanone and acetaldehyde at a molar ratio of 1 to 3 was introduced into the same reaction tube as in Example 8 packed with 15 ml. of the resulting catalyst at a flow rate of i mL/hr. at 550 C. for 10 hours. The organic layer separated from the liquid products was found to contain 74.8% of 2,6- diethylphenoi, 13.3% of o-ethyiphenoi and 2.1% of tristhyiphenol.

EXAMPLE l3 EXAMPLE 14 to 19 An aqueous solution containing cyciohexanone and formaldehyde at a molar ratio of l to 3 was introduced into the same reaction tube as in Example I packed with g of the catalysts prepared in the same manner as in Example I and maintained at 450 C. at a flow rate of i5 ml./hr. for 8 hours in the same manner as in Example 1. The results are tabulated in Table 6.

a. as a catalyst, at least one member of the group consisting of lithium carbonate, sodium carbonate, potassium carbonate, rubidium carbonate, cesium carbonate, lithium bicarbonate, sodium bicarbonate, potassium bicarbonate. rubidium bicarbonate, cesium bicarbonate, lithium nitrate, sodium nitrate, potassium nitrate, rubidium nitrate, cesium nitrate, lithium oxide, sodium oxide, potassium oxide, rubidium oxide, cesium oxide, lithium hydroxide, sodium hydroxide, potassium hydroxide, rubidium hydroxide, cesium hydroxide, lithium methoxide, sodium methoxide, potassium methoxide, lithium phenoxide, sodium phenoxide, potassium phenoxide, sodium formate, lithium acetate, potassium acetate, sodium axetyl acetonate, sodium salt of ethyl acetoacetic acid and as a promoter, at least one member of the group consisting of tin (ll) oxide, tin (IV) oxide, lead (ll) oxide, antimony (ill) oxide, bismuth (ill) oxide, arsenic (Ill) oxide, germanium (ll) oxide, lead (ll) carbonate, bismuth (ill) carbonate, germanium (ll) chloride, tin (IV) chloride, lead (ll) chloride, bismuth (ill) chloride, antimony (ill) chloride, arsenic (U-chloride, germanium i V) acetate, tin (IV) acetate, arsenic ("U-acetate, bismuth (III) acetate, lead (11) nitrate, tin (ll) nitrate and bismuth (IIl) nitrate.

2. The process of claim 1, wherein said reaction is effected at alsm sra qs m 250196991 C TABLE 6 Yield based on cyelohsxanone Ratio of Conver- (moi percent) recovery sion 01 of liquid cycio- 2,6- 2,4- 2,4,6- products hexanone ditri Example (weight (moi methylmethylmethyl- Number Catalyst percent) percent) o-Cresol phenol phenol phenol 15 K0 i 0 H3 90 99 8 7 5 2 3 16 NaOCHa 92 100 5 77 2 1 17 bN a 85 100 11 69 l 1 18 NaHCOa 88 100 11 75 1 3 19 CH3C=CHO0OH3 88 999 4 81 3 EXAMPLE 20 to 25 3. The process of claim 1, wherein said catalyst is supported Two hundred milliliters of an aqueous solution containing 9.5g of formaldehyde and 10.5g of cyclohexanone was continuously introduced into the same reactor as in Example 8 packed with 15 mi. of the catalysts prepared in the same manner as in Example 8 and maintained at 450 C. under the same conditions as in Example 8. The results are shown in Table 7. i

TABLE 7.

on a carrier selected from the group consisting of silica-gel, alumina, activated carbon, silica-alumina, zinc oxide, boria and silica-boria.

4. The process of claim 1, wherein 3 to 10 moles of the aldehyde are used for 1 mole of cyclohexanone.

5. The process of claim 1, wherein the amount of the catalyst ranges from 0.01 to 10g. based on lg. of the flowing yolume of cyclohe xanone andth e aldehyde Ratio of Yield based on cyclohexanone recovery of Conversion (moi percent) liquid of cycloproducts hexanone 2,6-di- 2,4-di- 2.4 6411- weight m0l methylmethyimethyl Example Number Catalyst Promoter percent percent o-Cresol phenol phenol phenol K=O GeCli 94 100 10' 79 2 Do PbCl, 94 100 4 83 2 D0 BKNOs); 97 99 3 88 2 Na,o As(OCCH 93 100 3 i ll 0 24 Do SbCL, 98 I00 3 89 25 Do SnO, 97 100 6 83 What is claimed is: 70 6. The process of claim 2, wherein the amount of the l. The process for the preparation of a 2,6-dialkylphenoi which comprises reacting cyclohexanone with either formaldehyde or acetaldehyde in the vapor phase at a temperature of from to 850C. in the presence of,

promoter ranges from 0.5 to 20 percent by weight of the amount of the catalyst. 

2. The process of claim 1, wherein said reaction is effected at a temperature of from 250* to 650* C.
 3. The process of claim 1, wherein said catalyst is supported on a carrier selected from the group consisting of silica-gel, alumina, activated carbon, silica-alumina, zinc oxide, boria and silica-boria.
 4. The process of claim 1, wherein 3 to 10 moles of the aldehyde are used for 1 mole of cyclohexanone.
 5. The process of claim 1, wherein the amount of the catalyst ranges from 0.01 to 10g. based on 1g. of the flowing volume of cyclohexanone and the aldehyde.
 6. The process of claim 2, wherein the amount of the promoter ranges from 0.5 to 20 percent by weight of the amount of the catalyst. 